Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C7/00—Purification; Separation; Use of additives
  • C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C7/00—Purification; Separation; Use of additives
  • C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
  • C07C7/14833—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound with metals or their inorganic compounds
  • C07C7/1485—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound with metals or their inorganic compounds oxides; hydroxides; salts
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P30/00—Technologies relating to oil refining and petrochemical industry
  • Y02P30/40—Ethylene production

Definitions

• the present invention relates to a process for removing arsenic, present in the form of arsenic hydride or arsine, from light olefin-containing hydrocarbons. More particularly, the present invention relates to a process for the removal of arsine from hydrocarbon feedstocks containing propylene.
• the light olefin-containing hydrocarbon feedstocks normally contain a small quantity of arsine.
• arsine is present to the extent of only several hundred parts per million (ppm) by weight. However, even this small amount is normally beyond the allowable limits of an acceptable product.
• arsine Even at very low concentrations, oftentimes renders olefins valueless for many purposes.
• high purity olefins are required for the satisfactory production of many polymeric products, especially those useful as plastics, including polymers of ethylene, propylene, and the like.
• arsine is a powerful reducing agent which appears able to reduce the olefin polymerization catalysts and cause their deactivation.
• Some of the known methods for removing arsine from light olefin containing hydrocarbon streams include the following.
• U.S. Pat. No. 3,782,076 (Carr et al., assigned to GULF R & D) discloses a process for reducing the arsenic content, believed to be present as arsine, from gaseous hydrocarbon streams by contacting said streams with supported lead oxide; however, the presence of sulfur compounds is said to interfere with the removal of arsine, and further the supported lead oxide may not be regenerated when sulfur compounds are present in the feed.
• U.S. Pat. No. 3,833,498 discloses a process for reducing the arsenic content, believed to be present as arsine, from gaseous hydrocarbon streams by contacting said streams with activated carbon derived from a bituminous coal and containing cobalt, nickel, molybdenum and vanadium.
• the feed should be substantially dry and free of sulfur compounds.
• the present invention is directed to a process for the removal of arsine from light olefin-containing hydrocarbon feedstocks, and more particularly from hydrocarbon feedstocks containing propylene and from about 0.06 to 150 ppm by weight of arsine.
• arsine is removed by passing the hydrocarbon feed over an absorbent material comprising nickel deposited on a support material and wherein the nickel is present in the forms of metallic nickel and nickel oxide.
• the total weight of nickel and nickel oxide can range up to about 80% by weight of the absorbent, with the provision that metallic nickel content is within the range of 10 wt. %-50 wt. % of the absorbent.
• the present invention relates to the removal of arsenic hydride, often referred to as arsine, from light olefin-containing hydrocarbon streams.
• Light olefins are C 2 -C 6 olefins.
• Of particular interest is the treatment of hydrocarbon streams containing light olefins which are to be subsequently subjected to polymerization using polymerization catalysts.
• hydrocarbon streams containing propylene present a special problem because of the closely related boiling points of propylene and arsine.
• stibine In addition to arsine, another possible contaminant of hydrocarbon is stibine (5bH 3 ). Stibine is less stable than arsine and is not formed readily. However, based upon the experimental data set forth below, it is believed that, in addition to arsine, the present invention will also result in the removal of stibine from feedstocks of the type described herein.
• the arsine removal process of the present invention reduces the arsine concentration in the treated hydrocarbon feedstock to 50 parts per billion by weight (ppb) or lower.
• the original arsine concentration may be as high as 1000 parts per million by weight (ppm) or higher depending on the process of making and the origin of the hydrocarbon feedstock. Due to the expense and specialization of the present invention, it is preferred to utilize other less costly and less complex processes to reduce the arsine concentration to 70 ppm or less prior to treatment in accordance with the present invention.
• the absorbent material used in the present invention comprises nickel deposited on a support material, the nickel being present both as metallic nickel and as nickel oxide.
• Silica, silica-aluminas, alumina, kieselguhr, zeolites and other similar materials, whether amorphous or crystalline, can be utilized as the support.
• the total weight of nickel and nickel oxide may represent up to about 80 wt. % of the absorbent material, with the provision that metallic nickel should not represent less than 10 wt. % nor more than 50 wt. % of the absorbent.
• the absorbent includes 20 wt. % or more of the support material.
• the weight ratio of metallic nickel to nickel oxide is of about 0.4 to about 2.0, and the absorbent comprises from about 30 to about 60 wt.
• the nickel can be deposited on the support by any suitable technique. Several methods well known to those skilled in the art. For example, nickel can be deposited on the support by dissolving nickel nitrate in water, mixing the solution with the support and precipitating the nickel, for example in the form of nickel carbonate, and subsequently washing, drying and calcining the precipitate. The nickel deposited in this manner is then partially reduced by means of hydrogen to form metallic nickel, the remainder being in the form of nickel oxide.
• the size of the nickel crystallites after reduction is from about 1 to about 20 nanometers nm). A more specific size range is about 1-2 nanometers.
• the size of the nickel crystallites depends on the extent of reduction carried out. In fact, if the degree of reduction is increased excessively, the size of the crystallites is increased to above the aforementioned range but the absorbent material obtained does not have the preferred properties. On the other hand, if the degree of reduction is too low, the crystallites still have good dimensions but the quantity of nickel available in this case is too small to ensure successful purification of the feedstock.
• the specific surface area of the absorbent material obtained after reduction is generally between 100 and 200 m 2 /g.
• the particle size of the absorbent material depends especially on the pressure drop allowed in the reactor; it has been noted, however, that it is advantageous to use the absorbent material in finely divided form.
• the particle diameter of this material when spherical does not exceed about 3.5 mm and is most preferably from about 1 to about 2.5 mm; when cylindrical particles are used, they preferably have a diameter of from about 1 to about 2 mm and a length from about 3 to about 8 mm.
• arsine can react with the metallic nickel and/or with nickel oxide, forming arsenic metal, which either forms a NiAs alloy or is deposited on the support.
• the absorbent material is usually prepared ex situ and stored either under a convenient saturated liquid hydrocarbon, like cyclohexane or dodecane or under a non-oxidizing atmosphere like CO 2 or N 2 .
• the temperature rise may be very significant, more particularly at the surface of the material at which the temperature may be much higher than that measured with a thermocouple, and it may thus damage the absorbent material.
• the high temperatures cause undesired side reactions, more particularly propylene dimerization and trimerization.
• the dimers are hexenes which copolymerize with propylene and break the regularity of the linear chain of isotactic polypropylene.
• the copolymer has a lower crystallinity than polypropylene, and thus a lower melting point; its mechanical resistance is also lower.
• an excessive increase in the temperature of the absorbent material can be avoided by previously conditioning the material by passing over said material an inert gas flow containing a minor amount of at least one light olefin, preferably propylene in a concentration of from about 0.1 to 5 vol %.
• the inert gas which should be oxygen free (contain the least possible amount of oxygen), is usually nitrogen. It is preferable to begin the conditioning procedure by passing essentially pure inert gas.
• the conditioning step is preferably carried out at about atmospheric pressure and at or below ambient temperature. It is continued until the propylene concentration at the outlet equals that introduced. It is also possible to monitor the passage of an exotherm, shown by thermocouples introduced within the absorbent material.
• the propylene feedstock contains less than 50 ppb and preferably less than 30 ppb of arsine. It has been unexpectedly found that by passing the propylene feedstock over an absorbent material as herein before described, the feedstock obtained has an arsine content not exceeding 50 ppb. This result is unexpected due to the degree of purity obtained and due to the fact that this process can be carried out either in the presence or in the absence of water.
• the hydrocarbon feedstock generally comprises more than 75 wt. % propylene, more particularly from about 85 to about 99 wt. % propylene, and up to about 10 ppm arsine.
• the propylene feedstock is passed over the absorbent material at a temperature of from about -10° C. to about 80° C., preferably of from about 10° C. to about 40° C., and under sufficient pressure to keep the medium in the liquid phase.
• the weight hourly space velocity (WHSV) utilized is from about 0.1 to about 25 kg/kg.h and preferably from about 1 to about 10 kg/kg.h.
• the hydrocarbon feedstock generally comprises more than 80 wt. % of ethylene, more particularly from about 90 to about 99 wt. %, and up to about 10 ppm of arsine.
• the ethylene temperature of from about -10° C. to about 80° C., preferably from about 10° C. to about 40° C., under a pressure of at least 1 MPa (10 Bars), and with a WHSV of from about 0.1 to about 25 kg/kg.h, preferably of from about 1 to about 10 kg/kg.h.
• a liquid hydrocarbon feedstock containing 99.5% of propylene, less than 5 ppm of water, and having a residual arsine content of 150,000 ppb was passed over an absorbent material consisting of 43.3% by weight of silica-alumina as the support, on which nickel was deposited, the nickel being present in the form of NiO and of metallic Ni, the weight ratio of metallic nickel to nickel oxide being of 0.668.
• the absorbent material contained about 49% by weight nickel.
• the absorbent material was finely divided to give an average particle size of about 1 mm.
• the specific surface area of this material was 145 m 2 /g, while its bulk density was of 0.81. It was stored under cyclohexane.
• the above-mentioned feedstock was passed in the upflow mode through the absorbent material at a temperature of 25° C., under a pressure of 1.5 MPa (15 bars) sufficient to keep the feedstock in the liquid phase and at a WHSV of 3.7 kg/kg.h.
• the purified feedstock had an arsine content as shown in Table I. Assuming that all arsine was absorbed during the first 96 hours, the capacity of the absorbent may thus be calculated to be of at least 53 g arsine/kg absorbent.
• a liquid hydrocarbon feedstock containing 99 wt. % propylene, 10 ppm of water and having a residual arsine content of 305 ppb was passed over the same absorbent material as in Example 1, at a temperature of 20° C., a pressure of 1.5 MPa (15 bars) sufficient to keep the feedstock in the liquid phase, and at a WHSV of 6 kg/kg.h. After 24 hours, the purified feedstock still had an arsine content lower than 3 ppb, even though the feed contained water.
• a polymerization test was carried out, using a Ziegler-type catalyst. Under identical conditions, the yield, expressed as the weight ratio of polypropylene to catalyst, was of 10,000 for the unpurified feed and of 32,000 for the purified feedstock.
• a liquid hydrocarbon feedstock containing 95.6 wt. % propylene, 3.8 wt. % propane and 0.6 wt. % C 4 hydrocarbons, the water content of which was about 30 ppm, and having a residual arsine content of 60 ppb was passed over the same absorbent as described in Example 1. This example is given to illustrate the activity of the absorbent over a long period of time.
• the feedstock was passed under a pressure of 1.5 MPa (15 bars), at a temperature of 24° C., and with a WHSV of 6 kg/kg.h.
• An absorbent material as described in Example 1 was prepared and stored under carbon dioxide for one month.
• the absorbent material was pretreated by passing a gaseous flow thereon, at a temperature of 180° C. and under atmospheric pressure, said gaseous flow being formed first of nitrogen during 14 hours, then a mixture of nitrogen and hydrogen during a further 24 hours, the hydrogen concentration therein being increased by about 5 vol % per hour up to more than 95 vol %.
• the absorbent material was cooled under said flow of nitrogen and hydrogen, then purged free of hydrogen with a nitrogen flow.
• the absorbent material was then conditioned.
• a nitrogen flow was passed during 4 hours over the absorbent material, under atmospheric pressure, at a temperature of 20° C., and with a gaseous hourly space velocity (GHSV) of 125 l/l.h.
• GHSV gaseous hourly space velocity
• Example 1 The purification procedure of Example 1 was repeated with the conditioned material. Results similar to Example 1 were obtained and the purified feedstock had an arsine content as shown in Table III at the conclusion of the periods indicated.

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• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Engineering & Computer Science (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Analytical Chemistry (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Water Supply & Treatment (AREA)
• General Chemical & Material Sciences (AREA)
• Inorganic Chemistry (AREA)
• Solid-Sorbent Or Filter-Aiding Compositions (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Manufacture And Refinement Of Metals (AREA)
• Inorganic Compounds Of Heavy Metals (AREA)
• Separation Of Gases By Adsorption (AREA)
• Treatment Of Liquids With Adsorbents In General (AREA)
• Treating Waste Gases (AREA)
• Carbon And Carbon Compounds (AREA)

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Citations (10)

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• 1987
  • 1987-09-24 EP EP87870137A patent/EP0308569B1/en not_active Expired - Lifetime
  • 1987-09-24 AT AT87870137T patent/ATE73118T1/de not_active IP Right Cessation
  • 1987-09-24 ES ES198787870137T patent/ES2038695T3/es not_active Expired - Lifetime
  • 1987-09-24 DE DE8787870137T patent/DE3777182D1/de not_active Expired - Lifetime
• 1988
  • 1988-09-13 NO NO884051A patent/NO177421C/no not_active IP Right Cessation
  • 1988-09-21 CA CA000577973A patent/CA1314689C/en not_active Expired - Lifetime
  • 1988-09-22 JP JP63236639A patent/JPH0832641B2/ja not_active Expired - Fee Related
  • 1988-09-23 MX MX013144A patent/MX168866B/es unknown
  • 1988-09-23 US US07/248,533 patent/US4861939A/en not_active Expired - Lifetime
  • 1988-09-23 PT PT88582A patent/PT88582B/pt not_active IP Right Cessation
  • 1988-09-23 RU SU884356563A patent/RU2007437C1/ru active
  • 1988-09-23 AU AU22742/88A patent/AU654260B2/en not_active Expired
  • 1988-09-24 KR KR1019880012438A patent/KR960016465B1/ko not_active Expired - Lifetime
  • 1988-09-24 CN CN88107409A patent/CN1014402B/zh not_active Expired
• 1992
  • 1992-03-05 GR GR910402025T patent/GR3003972T3/el unknown

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